CN106117018A - The method of phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery - Google Patents
The method of phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery Download PDFInfo
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- CN106117018A CN106117018A CN201610520456.XA CN201610520456A CN106117018A CN 106117018 A CN106117018 A CN 106117018A CN 201610520456 A CN201610520456 A CN 201610520456A CN 106117018 A CN106117018 A CN 106117018A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C37/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring
- C07C37/08—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom of a six-membered aromatic ring by decomposition of hydroperoxides, e.g. cumene hydroperoxide
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C407/00—Preparation of peroxy compounds
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
- C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
- C07C45/53—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition of hydroperoxides
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
A kind of method that the present invention relates to phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, mainly solves the problem that in prior art, energy consumption is higher.The present invention is by a kind of method using phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, oxidation reactor charging and one-level concentration tower is used to eject material technological means of heat exchange in the heat exchanger of one-level concentration tower top, reach to reduce low low-pressure steam 0.21 kg/kg phenol, reduce the technical purpose of cooling water 11.0 kg/kg phenol, and nominal situation can be suitable for, driving operating mode, the technical scheme of operating mode of stopping in emergency different condition operation running preferably solves the problems referred to above, can be used in phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery.
Description
Technical field
A kind of method that the present invention relates to phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery.
Background technology
Phenol is the colourless acicular crystal with special odor, is a kind of multiduty Chemical Manufacture raw material.Acetone is one
Plant the chemical solvent of common highly volatile.Number of patent application US20110301384A1 cumene oxidation system and patent Shen
Please the manufacture method of number CN200580006398.9 cumene hydroperoxide, describe and carry out isopropylbenzene with dry method and contain in a wet process
Carrier of oxygen carries out oxidation reaction, the technique preparing cumyl hydroperoxide.Number of patent application CN201410719776.9 reduces benzene
The method of phenol acetone device oxidation reaction unit energy consumption, disclose oxidation charging cumene stream by oxidizing tower heat exchanger with
Reflux stream heat exchange at the bottom of oxidizing tower, further enters oxidizing tower and reacts after preheating, reach to recycle heat of reaction, have
Effect reduces the method for energy consumption purpose.Number of patent application CN201410719763.1 phenol-acetone device oxidation reaction unit reduces energy
The method of consumption, discloses oxidation charging cumene stream and successively passes through 2# oxidizing tower heat exchanger and 1# oxidizing tower heat exchanger,
Respectively with 2# and 1# oxidizing tower at the bottom of reflux stream heat exchange, further preheating after enter oxidizing tower react, reach reclaim profit
Method by heat of reaction, effectively reduction energy consumption purpose.The method of patent No. WO2014153040A2 acetone and phenol with
System, a kind of method describing acetone and phenol, during crude acetone column acetone and phenol, use crude acetone
Top gaseous phase pre-thermal oxide charging isopropylbenzene reaches the purpose of Appropriate application heat energy.
Prior art generates cumyl hydroperoxide at isopropylbenzene dry process reaction, during preparing phenol-acetone, at oxygen
Changing unit and arrange an oxidation feed preheater, the isopropylbenzene charging of oxidizing tower is preheated to most preferably feed temperature with low low-pressure steam
Degree.Meanwhile, at cumyl hydroperoxide concentration unit, one-level concentration tower top gas phase discharging cooling water section is condensed into liquid
Phase, liquid-phase reflux feeds workshop section's isopropylbenzene alkaline bath to oxidation, and gas phase enters concentration tail gas cryoprobe and condenses further.Oxidizing tower
Feeding preheating needs to consume a large amount of low low-pressure steam, and the condensation of one-level concentration top gaseous phase then needs to consume and cools down water in a large number, deposits
Big at utility consumption, the problems such as Energy harvesting is unreasonable.
Summary of the invention
The technical problem to be solved is the problem that in prior art, energy consumption is higher, it is provided that a kind of new phenol third
The method of ketone device cumyl hydroperoxide upgrading system waste heat recovery.The method has the advantage that energy consumption is relatively low.
For solving the problems referred to above, the technical solution used in the present invention is as follows: a kind of phenol-acetone device hydrogen peroxide isopropyl
The method of benzene upgrading system waste heat recovery, isopropylbenzene material (2) is by one-level concentration tower top heat exchanger (22) and one-level concentration tower
Top gas light component (6) mutually carries out heat exchange, and the isopropylbenzene material (4) after heating is preheated to charging by oxidation feed preheater (21)
Entering the air material (15) being passed through in oxidation reactor (25), with reactor after temperature occurs oxidation reaction to generate hydrogen peroxide
Isopropylbenzene (16), the oxidized tail gas (17) generated in oxidation reactor (25) send oxidized tail gas condenser；Fresh isopropylbenzene (18)
Carrying out material rectification with the material (19) entrance one-level concentration tower (26) carrying out autoxidation blow tank to separate, tower reactor heavy constituent (20) is sent
Two grades of concentration towers, the light component of one-level concentration top gaseous phase (6) first in one-level concentration tower top heat exchanger (22) with isopropylbenzene thing
Material (2) heat exchange, then one-level concentration overhead condenser (23) the continuation condensation through series connection, uncooled gaseous phase materials (8) enters
Concentration tail gas cryoprobe (24) condenses further, and in concentration tail gas cryoprobe (24), to deliver to concentration true for uncooled fixed gas (9)
Empty spraying system；The condensed fluid (12) formed in one-level concentration overhead condenser (23) and concentration tail gas cryoprobe (24) are formed
Condensed fluid (13) merge into material (14) and remove isopropylbenzene alkaline bath；During nominal situation, one-level concentration tower top heat exchanger (22) is cold
The valve (10) of side parallel connection by-pass line is the normally off, and the valve (11) of hot side parallel connection by-pass line is the normally off, oxidation reaction charging isopropyl
Benzene material (2) and the light component of one-level concentration top gaseous phase (6) carry out heat exchange；During driving operating mode, open bypass valve (10), isopropyl
Benzene material (2) flows through from this bypass valve (10), and oxidation charging isopropylbenzene (4) carries out pre-by oxidation feed preheater (21)
Heat；During operating mode of stopping in emergency, opening bypass valve (11), the light component of one-level concentration top gaseous phase (6) is from this bypass valve (11)
Flowing through, one-level concentration top gaseous phase (7) condenses through one-level concentration overhead condenser (23), enters back into concentration tail gas cryoprobe
(24) condense further.
In technique scheme, it is preferable that heat exchanger (22) hot side, one-level concentration tower top operation temperature is 60～100 DEG C；
Operation gauge pressure is 0.005～0.020MPa；Cold side operation temperature is 30～90 DEG C；Operation gauge pressure is 0.3～1.5MPa；One-level carries
Dense overhead condenser hot side operation temperature is 40～80 DEG C；Operation gauge pressure is 0.005～0.020MPa；Oxidation feed preheater
(21) operation temperature in cold side is 30～110 DEG C；Operation gauge pressure is 0.3～1.5MPa.
In technique scheme, it is highly preferred that heat exchanger (22) hot side, one-level concentration tower top operation temperature is 65～95 DEG C；
Operation gauge pressure is 0.008～0.018MPa；Cold side operation temperature is 35～85 DEG C；Operation gauge pressure is 0.5～1.2MPa；One-level carries
Dense overhead condenser (23) hot side operation temperature is 45～75 DEG C；Operation gauge pressure is 0.008～0.018MPa；Oxidation feeding preheating
Device (21) cold side operation temperature is 40～105 DEG C；Operation gauge pressure is 0.5～1.2MPa.
In technique scheme, most preferably, operation temperature in one-level concentration tower top heat exchanger (22) hot side is 70～90 DEG C；
Operation gauge pressure is 0.010～0.015MPa；Cold side operation temperature is 40～80 DEG C；Operation gauge pressure is 0.6～1.0MPa；One-level carries
Dense overhead condenser (23) hot side operation temperature is 50～70 DEG C；Operation gauge pressure is 0.010～0.015MPa；Oxidation feeding preheating
Device (21) cold side operation temperature is 50～100 DEG C；Operation gauge pressure is 0.6～1.0MPa.
In technique scheme, it is preferable that oxidation feed preheater (21) uses low low-pressure steam to preheat；One-level concentration tower
Cooling water condensation is used on top condenser (23)；Concentration tail gas cryoprobe (24) condenses with chilled water.
In technique scheme, it is preferable that the reaction condition of oxidation reactor (25): operation temperature is 80～110 DEG C, behaviour
It is 0.2～0.4MPa as gauge pressure；The mass ratio that isopropylbenzene (5) charging and compressed air (15) feed is: isopropylbenzene: air=10
～20:1；Isopropylbenzene conversion per pass is 3.2～8.5%.
In technique scheme, it is preferable that isopropylbenzene (5) feeding temperature is 80～110 DEG C.
In technique scheme, it is preferable that the operating condition of one-level concentration tower (26): operation temperature is 90～170 DEG C, behaviour
It is 0.015～0.035MPa as gauge pressure.
In technique scheme, it is preferable that the operating condition of concentration tail gas cryoprobe (24): operation temperature is 20～50
DEG C, operation absolute pressure is 0.010～0.020MPa.
The isopropylbenzene that oxidation reactor is fed by the present invention heats in the heat exchanger of one-level concentration tower top, enter back into aoxidize into
Material preheater utilizes low low-pressure steam to continue to be preheated to optimal feeding temperature；One-level concentration top gaseous phase is also at one-level concentration simultaneously
Tower top heat exchanger condenses, then utilizes cooling water to continue condensation through one-level concentration overhead condenser；One-level concentration tower takes one's place heat
Device heat exchange amount is 112.3 kcal/kg phenol.Thus can reduce low low-pressure steam and consume 0.21 kg/kg phenol, reduce
Cooling-water consumption 11.0 kg/kg phenol, and the present invention can be suitable for nominal situation, operating mode of driving, operating mode of stopping in emergency
Etc. the operation running of different condition, achieve preferable technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1, oxidation reaction charging；2, isopropylbenzene material；3, the isopropylbenzene after the heat exchanger heat exchange of one-level concentration tower top
Material；4, through the isopropylbenzene material of bypass valve 10；5, the isopropylbenzene material after the preheating of oxidation feed preheater；6, one-level carries
The light component of dense top gaseous phase；7, one-level concentration tower top condenser inlet material；8, one-level concentration tower top condensator outlet gas gas-phase objects
Material；9, fixed gas；10, valve；11, valve；12, one-level concentration tower top condensator outlet condensed fluid；13, concentration tail gas cryoprobe
Condensed fluid；14, the material of isopropylbenzene alkaline bath is removed；15, air material；16, cumyl hydroperoxide；17, oxidized tail gas；
18, fresh isopropylbenzene；19, the material of autoxidation blow tank is carried out；20, one-level concentration tower reactor heavy constituent；21, oxidation feeding preheating
Device；22, one-level concentration tower top heat exchanger；23, one-level concentration overhead condenser；24, concentration tail gas cryoprobe；25, oxidation reaction
Device；26, one-level concentration tower.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Detailed description of the invention
[embodiment 1]
A kind of method of phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, as it is shown in figure 1, isopropylbenzene
Material (2) carries out heat exchange, after heating by one-level concentration tower top heat exchanger (22) and the light component of one-level concentration top gaseous phase (6)
Isopropylbenzene material (4) enters oxidation reactor (25), with reaction after being preheated to feeding temperature by oxidation feed preheater (21)
The air material (15) being passed through in device occurs oxidation reaction to generate generation in cumyl hydroperoxide (16), oxidation reactor (25)
Oxidized tail gas (17) send oxidized tail gas condenser；Fresh isopropylbenzene (18) and come autoxidation blow tank material (19) enter one
Level concentration tower (26) carries out material rectification separation, and tower reactor heavy constituent (20) send two grades of concentration towers, light group of one-level concentration top gaseous phase
Point (6) first in one-level concentration tower top heat exchanger (22) with isopropylbenzene material (2) heat exchange, then the one-level concentration tower top through series connection
Condenser (23) continues condensation, and uncooled gaseous phase materials (8) enters concentration tail gas cryoprobe (24) and condenses further, concentration tail
In gas cryoprobe (24), uncooled fixed gas (9) delivers to concentration airless injection system；In one-level concentration overhead condenser (23)
The condensed fluid (13) formed in the condensed fluid (12) formed and concentration tail gas cryoprobe (24) is merged into material (14) and is removed isopropylbenzene
Alkaline bath；During nominal situation, the valve (10) of one-level concentration tower top heat exchanger (22) cold side parallel connection by-pass line is the normally off, and hot side is also
The valve (11) of connection by-pass line is the normally off, oxidation reaction charging isopropylbenzene material (2) and the light component of one-level concentration top gaseous phase (6)
Carry out heat exchange；During driving operating mode, opening bypass valve (10), isopropylbenzene material (2) flows through from this bypass valve (10), aoxidize into
Material isopropylbenzene (4) is preheated by oxidation feed preheater (21)；During operating mode of stopping in emergency, open bypass valve (11), one
The level light component of concentration top gaseous phase (6) flows through from this bypass valve (11), and one-level concentration top gaseous phase (7) is through one-level concentration tower
Top condenser (23) condensation, enters back into concentration tail gas cryoprobe (24) and condenses further.
The production scale of phenol-acetone device is 100,000 tons/year, uses the cumyl hydroperoxide upgrading system of the present invention
The method of waste heat recovery, process operation parameter is: newly-increased exchanger heat side, one-level concentration tower top operation temperature is 75 DEG C, operation
Pressure (gauge pressure) is 0.010MPa；Cold side operation temperature is 30 DEG C, and operation pressure (gauge pressure) is 0.9MPa.One-level concentration tower top is cold
Condenser hot side operation temperature is 45 DEG C, and operation pressure (gauge pressure) is 0.010MPa.Operation temperature in oxidation feed preheater cold side is
50 DEG C, operation pressure (gauge pressure) is 0.9MPa.Oxidation reactor operation temperature is 102 DEG C, and operation pressure (gauge pressure) is
0.32MPa；Isopropylbenzene charging is isopropylbenzene with the mass ratio of compressed air charging: air=16.5:1；Isopropylbenzene conversion per pass
Rate is 5.5%.Isopropylbenzene feeding temperature is 102 DEG C.One-level concentration tower tower top operation temperature is 95 DEG C, and tower reactor operation temperature is
155 DEG C, operation pressure (gauge pressure) is 0.028MPa.Concentration tail gas cryoprobe operation temperature is 30 DEG C, and operation pressure (absolute pressure) is
0.013MPa.Thus, reduce low low-pressure steam consume 1.64 ton hour and reduce cooling-water consumption 86.0 ton hour.
[embodiment 2]
According to the condition described in embodiment 1 and step, simply phenol-acetone production scale changes 200,000 tons/year into.Use this
The method of the cumyl hydroperoxide upgrading system waste heat recovery of invention, process operation parameter is: newly-increased one-level concentration tower top
Exchanger heat side operation temperature is 95 DEG C, and operation pressure (gauge pressure) is 0.010MPa；Cold side operation temperature is 50 DEG C, operates pressure
(gauge pressure) is 0.9MPa.One-level concentration overhead condenser hot side operation temperature is 75 DEG C, and operation pressure (gauge pressure) is 0.010MPa.
Operation temperature in oxidation feed preheater cold side is 105 DEG C, and operation pressure (gauge pressure) is 0.9MPa.Oxidation reactor operation temperature is
105 DEG C, operation pressure (gauge pressure) is 0.35MPa；Isopropylbenzene charging is isopropylbenzene with the mass ratio of compressed air charging: air=
18.2:1；Isopropylbenzene conversion per pass is 5.9%.Isopropylbenzene feeding temperature is 105 DEG C.One-level concentration tower tower top operation temperature is
101 DEG C, tower reactor operation temperature is 163 DEG C, and operation pressure (gauge pressure) is 0.032MPa.Concentration tail gas cryoprobe operation temperature is 42
DEG C, operation pressure (absolute pressure) is 0.017MPa.Thus, reduce low low-pressure steam consume 3.28 ton hour and reduce cooling water disappear
Consume 171.9 ton hour.
[embodiment 3]
According to the condition described in embodiment 1 and step, simply phenol-acetone production scale changes 350,000 tons/year into.Use this
The method of the cumyl hydroperoxide upgrading system waste heat recovery of invention, process operation parameter is: newly-increased one-level concentration tower top
Exchanger heat side operation temperature is 85 DEG C, and operation pressure (gauge pressure) is 0.010MPa；Cold side operation temperature is 40 DEG C, operates pressure
(gauge pressure) is 0.9MPa.One-level concentration overhead condenser hot side operation temperature is 55 DEG C, and operation pressure (gauge pressure) is 0.010MPa.
Operation temperature in oxidation feed preheater cold side is 75 DEG C, and operation pressure (gauge pressure) is 0.9MPa.Oxidation reactor operation temperature is
107 DEG C, operation pressure (gauge pressure) is 0.37MPa；Isopropylbenzene charging is isopropylbenzene with the mass ratio of compressed air charging: air=
17.9:1；Isopropylbenzene conversion per pass is 7.0%.Isopropylbenzene feeding temperature is 107 DEG C.One-level concentration tower tower top operation temperature is
109 DEG C, tower reactor operation temperature is 166 DEG C, and operation pressure (gauge pressure) is 0.033MPa.Concentration tail gas cryoprobe operation temperature is 46
DEG C, operation pressure (absolute pressure) is 0.019MPa.Thus, reduce low low-pressure steam consume 5.74 ton hour and reduce cooling water disappear
Consume 300.8 ton hour.
[embodiment 4]
According to the condition described in embodiment 1 and step, simply phenol-acetone production scale changes 400,000 tons/year into.Use this
The method of the cumyl hydroperoxide upgrading system waste heat recovery of invention, process operation parameter is: newly-increased one-level concentration tower top
Exchanger heat side operation temperature is 80 DEG C, and operation pressure (gauge pressure) is 0.010MPa；Cold side operation temperature is 40 DEG C, operates pressure
(gauge pressure) is 0.9MPa.One-level concentration overhead condenser hot side operation temperature is 50 DEG C, and operation pressure (gauge pressure) is 0.010MPa.
Operation temperature in oxidation feed preheater cold side is 68 DEG C, and operation pressure (gauge pressure) is 0.9MPa.Oxidation reactor operation temperature is
93 DEG C, operation pressure (gauge pressure) is 0.25MPa；Isopropylbenzene charging is isopropylbenzene with the mass ratio of compressed air charging: air=
13.2:1；Isopropylbenzene conversion per pass is 4.1%.Isopropylbenzene feeding temperature is 93 DEG C.One-level concentration tower tower top operation temperature is
91 DEG C, tower reactor operation temperature is 153 DEG C, and operation pressure (gauge pressure) is 0.016MPa.Concentration tail gas cryoprobe operation temperature is 22
DEG C, operation pressure (absolute pressure) is 0.011MPa.Thus, reduce low low-pressure steam consume 6.56 ton hour and reduce cooling water disappear
Consume 343.8 ton hour.
[embodiment 5]
According to the condition described in embodiment 4 and step, phenol-acetone production scale is 400,000 tons/year, simply technological operation
Parameter change.The method using the cumyl hydroperoxide upgrading system waste heat recovery of the present invention, process operation parameter is: newly-increased
Exchanger heat side, one-level concentration tower top operation temperature be 60 DEG C, operation pressure (gauge pressure) be 0.005MPa；Cold side operation temperature
Being 30 DEG C, operation pressure (gauge pressure) is 0.3MPa.One-level concentration overhead condenser hot side operation temperature is 40 DEG C, operates pressure
(gauge pressure) is 0.005MPa.Operation temperature in oxidation feed preheater cold side is 30 DEG C, and operation pressure (gauge pressure) is 0.3MPa.Oxidation
Reactor operation temperature is 80 DEG C, and operation pressure (gauge pressure) is 0.2MPa；The mass ratio that isopropylbenzene charging feeds with compressed air
For isopropylbenzene: air=10:1；Isopropylbenzene conversion per pass is 3.2%.Isopropylbenzene feeding temperature is 80 DEG C.One-level concentration tower tower
Top operation temperature is 90 DEG C, and tower reactor operation temperature is 150 DEG C, and operation pressure (gauge pressure) is 0.015MPa.Concentration tail gas cryoprobe
Operation temperature is 20 DEG C, and operation pressure (absolute pressure) is 0.010MPa.Thus, reduce low low-pressure steam and consume 6.49 ton hour also
Reduce cooling-water consumption 347.2 ton hour.
[embodiment 6]
According to the condition described in embodiment 4 and step, phenol-acetone production scale is 400,000 tons/year, simply technological operation
Parameter change.The method using the cumyl hydroperoxide upgrading system waste heat recovery of the present invention, process operation parameter is: newly-increased
Exchanger heat side, one-level concentration tower top operation temperature be 100 DEG C, operation pressure (gauge pressure) be 0.020MPa；Cold side operation temperature
Being 90 DEG C, operation pressure (gauge pressure) is 1.5MPa.One-level concentration overhead condenser hot side operation temperature is 80 DEG C, operates pressure
(gauge pressure) is 0.020MPa.Operation temperature in oxidation feed preheater cold side is 110 DEG C, and operation pressure (gauge pressure) is 1.5MPa.Oxygen
Changing reactor operation temperature is 110 DEG C, and operation pressure (gauge pressure) is 0.4MPa；The quality that isopropylbenzene charging feeds with compressed air
Ratio is isopropylbenzene: air=20:1；Isopropylbenzene conversion per pass is 8.5%.Isopropylbenzene feeding temperature is 110 DEG C.One-level concentration
Column overhead operation temperature is 110 DEG C, and tower reactor operation temperature is 170 DEG C, and operation pressure (gauge pressure) is 0.035MPa.Concentration tail gas is cold
Freezing device operation temperature is 50 DEG C, and operation pressure (absolute pressure) is 0.020MPa.Thus, reduce low low-pressure steam consume 6.63 tons/little
Time and reduce cooling-water consumption 339.7 ton hour.
Obviously, the method using the present invention, mainly solve oxidation reactor feeding preheating and one-level concentration in prior art
Top gaseous phase condensation uses low low-pressure steam and cooling water respectively, there is public work and consumes the problems such as big, uses oxidation reaction
Device charging and one-level concentration tower eject material technological means of heat exchange in the heat exchanger of one-level concentration tower top, reach to reduce low pressure and steam
Vapour 0.21 kg/kg phenol, reduces the technical purpose of cooling water 11.0 kg/kg phenol, and the present invention can be suitable for
Nominal situation, operating mode of driving, the operation running of the different conditions such as operating mode of stopping in emergency, preferably solve this problem, can
It is applied to prepare in the commercial production of phenol-acetone.
Claims (9)
1. a method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, isopropylbenzene material (2) passes through
One-level concentration tower top heat exchanger (22) and the light component of one-level concentration top gaseous phase (6) carry out heat exchange, the isopropylbenzene material after heating
(4) it is passed through in entrance oxidation reactor (25), with reactor after being preheated to feeding temperature by oxidation feed preheater (21)
Air material (15) occurs oxidation reaction to generate the oxidized tail gas generated in cumyl hydroperoxide (16), oxidation reactor (25)
(17) oxidized tail gas condenser is sent；Fresh isopropylbenzene (18) and come autoxidation blow tank material (19) enter one-level concentration tower
(26) carrying out material rectification separation, tower reactor heavy constituent (20) send two grades of concentration towers, and the light component of one-level concentration top gaseous phase (6) first exists
With isopropylbenzene material (2) heat exchange in one-level concentration tower top heat exchanger (22), then the one-level concentration overhead condenser through series connection
(23) continuing condensation, uncooled gaseous phase materials (8) enters concentration tail gas cryoprobe (24) and condenses further, and concentration tail gas is freezing
In device (24), uncooled fixed gas (9) delivers to concentration airless injection system；One-level concentration overhead condenser (23) is formed
The condensed fluid (13) formed in condensed fluid (12) and concentration tail gas cryoprobe (24) is merged into material (14) and is removed isopropylbenzene alkaline bath；
During nominal situation, the valve (10) of one-level concentration tower top heat exchanger (22) cold side parallel connection by-pass line is the normally off, and the parallel connection of hot side bypasses
The valve (11) of pipeline is the normally off, and oxidation reaction charging isopropylbenzene material (2) is changed with the light component of one-level concentration top gaseous phase (6)
Heat；During driving operating mode, opening bypass valve (10), isopropylbenzene material (2) flows through from this bypass valve (10), oxidation charging isopropyl
Benzene (4) is preheated by oxidation feed preheater (21)；During operating mode of stopping in emergency, open bypass valve (11), one-level concentration
The light component of top gaseous phase (6) flows through from this bypass valve (11), and one-level concentration top gaseous phase (7) is through one-level concentration overhead condensation
Device (23) condenses, and enters back into concentration tail gas cryoprobe (24) and condenses further.
The most according to claim 1, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levy and be that heat exchanger (22) hot side, one-level concentration tower top operation temperature is 60～100 DEG C；Operation gauge pressure be 0.005～
0.020MPa；Cold side operation temperature is 30～90 DEG C；Operation gauge pressure is 0.3～1.5MPa；The hot side of one-level concentration overhead condenser
Operation temperature is 40～80 DEG C；Operation gauge pressure is 0.005～0.020MPa；Operation temperature in oxidation feed preheater (21) cold side is
30～110 DEG C；Operation gauge pressure is 0.3～1.5MPa.
The most according to claim 2, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levy and be that heat exchanger (22) hot side, one-level concentration tower top operation temperature is 65～95 DEG C；Operation gauge pressure is 0.008～0.018MPa；
Cold side operation temperature is 35～85 DEG C；Operation gauge pressure is 0.5～1.2MPa；One-level concentration overhead condenser (23) hot side operation temperature
Degree is 45～75 DEG C；Operation gauge pressure is 0.008～0.018MPa；Oxidation feed preheater (21) cold side operation temperature be 40～
105℃；Operation gauge pressure is 0.5～1.2MPa.
The most according to claim 3, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levy and be that heat exchanger (22) hot side, one-level concentration tower top operation temperature is 70～90 DEG C；Operation gauge pressure is 0.010～0.015MPa；
Cold side operation temperature is 40～80 DEG C；Operation gauge pressure is 0.6～1.0MPa；One-level concentration overhead condenser (23) hot side operation temperature
Degree is 50～70 DEG C；Operation gauge pressure is 0.010～0.015MPa；Oxidation feed preheater (21) cold side operation temperature be 50～
100℃；Operation gauge pressure is 0.6～1.0MPa.
The most according to claim 1, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levy and be that aoxidizing feed preheater (21) uses low low-pressure steam to preheat；One-level concentration overhead condenser (23) cooling water-cooled
Solidifying；Concentration tail gas cryoprobe (24) condenses with chilled water.
The most according to claim 1, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levying the reaction condition being oxidation reactor (25): operation temperature is 80～110 DEG C, operation gauge pressure is 0.2～0.4MPa；Isopropyl
The mass ratio that benzene (5) charging and compressed air (15) feed is: isopropylbenzene: air=10～20:1；Isopropylbenzene conversion per pass
It is 3.2～8.5%.
The most according to claim 1, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levy and be that isopropylbenzene (5) feeding temperature is 80～110 DEG C.
The most according to claim 1, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levying the operating condition being one-level concentration tower (26): operation temperature is 90～170 DEG C, operation gauge pressure is 0.015～0.035MPa.
The most according to claim 1, the method for phenol-acetone device cumyl hydroperoxide upgrading system waste heat recovery, it is special
Levy the operating condition being concentration tail gas cryoprobe (24): operation temperature is 20～50 DEG C, operation absolute pressure be 0.010～
0.020MPa。
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| CN111606834A (en) * | 2020-05-21 | 2020-09-01 | 常州瑞华化工工程技术股份有限公司 | Concentration method of ethylbenzene hydroperoxide |
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|---|---|---|---|---|
| CN104447214A (en) * | 2014-12-01 | 2015-03-25 | 中石化上海工程有限公司 | Method for reducing energy consumption by employing phenol-acetone device oxidation reaction unit |
| CN105246867A (en) * | 2013-03-14 | 2016-01-13 | 凯洛格·布朗及鲁特有限公司 | Methods and systems for separating acetone and phenol from one another |
| CN105237374A (en) * | 2015-10-12 | 2016-01-13 | 中石化上海工程有限公司 | Phenol-acetone device acetone refining system waste heat recovery method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105246867A (en) * | 2013-03-14 | 2016-01-13 | 凯洛格·布朗及鲁特有限公司 | Methods and systems for separating acetone and phenol from one another |
| CN104447214A (en) * | 2014-12-01 | 2015-03-25 | 中石化上海工程有限公司 | Method for reducing energy consumption by employing phenol-acetone device oxidation reaction unit |
| CN105237374A (en) * | 2015-10-12 | 2016-01-13 | 中石化上海工程有限公司 | Phenol-acetone device acetone refining system waste heat recovery method |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111606834A (en) * | 2020-05-21 | 2020-09-01 | 常州瑞华化工工程技术股份有限公司 | Concentration method of ethylbenzene hydroperoxide |
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